EP1816397B1 - Method and device for heat recovery, from humid exhaust air - Google Patents
Method and device for heat recovery, from humid exhaust air Download PDFInfo
- Publication number
- EP1816397B1 EP1816397B1 EP07101622.4A EP07101622A EP1816397B1 EP 1816397 B1 EP1816397 B1 EP 1816397B1 EP 07101622 A EP07101622 A EP 07101622A EP 1816397 B1 EP1816397 B1 EP 1816397B1
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- EP
- European Patent Office
- Prior art keywords
- heat
- cycle
- temperature
- low
- heat exchanger
- Prior art date
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- 238000000034 method Methods 0.000 title claims description 29
- 238000011084 recovery Methods 0.000 title description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 60
- 238000010791 quenching Methods 0.000 claims description 31
- 238000010521 absorption reaction Methods 0.000 claims description 25
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 17
- 239000006096 absorbing agent Substances 0.000 claims description 12
- 230000008878 coupling Effects 0.000 claims description 7
- 238000010168 coupling process Methods 0.000 claims description 7
- 238000005859 coupling reaction Methods 0.000 claims description 7
- 239000002912 waste gas Substances 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims 3
- 239000012530 fluid Substances 0.000 claims 1
- 238000009833 condensation Methods 0.000 description 18
- 230000005494 condensation Effects 0.000 description 18
- 239000007789 gas Substances 0.000 description 13
- 238000010438 heat treatment Methods 0.000 description 13
- 239000000243 solution Substances 0.000 description 9
- 238000001704 evaporation Methods 0.000 description 8
- 230000008020 evaporation Effects 0.000 description 7
- 238000011109 contamination Methods 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 238000000605 extraction Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 239000003507 refrigerant Substances 0.000 description 4
- 235000002639 sodium chloride Nutrition 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 238000004065 wastewater treatment Methods 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 239000012717 electrostatic precipitator Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 239000004449 solid propellant Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- 101100353161 Drosophila melanogaster prel gene Proteins 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000008236 heating water Substances 0.000 description 1
- 238000011086 high cleaning Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J15/00—Arrangements of devices for treating smoke or fumes
- F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/265—Drying gases or vapours by refrigeration (condensation)
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B23/00—Heating arrangements
- F26B23/001—Heating arrangements using waste heat
- F26B23/002—Heating arrangements using waste heat recovered from dryer exhaust gases
- F26B23/005—Heating arrangements using waste heat recovered from dryer exhaust gases using a closed cycle heat pump system ; using a heat pipe system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C3/00—Other direct-contact heat-exchange apparatus
- F28C3/06—Other direct-contact heat-exchange apparatus the heat-exchange media being a liquid and a gas or vapour
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
- F28D21/0012—Recuperative heat exchangers the heat being recuperated from waste water or from condensates
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2219/00—Treatment devices
- F23J2219/70—Condensing contaminants with coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES
- F23J2900/00—Special arrangements for conducting or purifying combustion fumes; Treatment of fumes or ashes
- F23J2900/15004—Preventing plume emission at chimney outlet
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/30—Technologies for a more efficient combustion or heat usage
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Definitions
- the invention relates to a method for heat recovery from accumulating in a drying process moisture-laden exhaust air, the heat is coupled as low-temperature heat in a designed as absorption heat pump, thermodynamic cycle, where it is raised to a higher temperature level and coupled on the high temperature level as useful heat and at the same time at least a portion of the moisture contained in the exhaust air is condensed.
- the invention relates to an apparatus for carrying out such a method
- the recovery of heat of condensation from an exhaust gas stream is already known from practice. It is used u.a. in industrial furnaces of various kinds, in solid fuel firing, dryers, flue gas cleaning plants, steam and hot water generators or similar plants in the industrial, commercial or public, such as municipal, area.
- the heat from the exhaust stream directly, from a Quenchigannikturiterrorism cooling the exhaust stream or from other liquid absorbate, such. Calcium hydroxide in flue gas desulfurization, ie by condensation while cleaning the exhaust gases are obtained.
- a method of the type mentioned is, for example, from EP 0 523 684 A1 known.
- the invention is therefore based on the object to increase the efficiency of heat recovery.
- the object is achieved by a method according to claim 1 and a device according to claim 10.
- the devices suitable for carrying out the thermodynamic cycle can be made compact. Normally, they are delivered as a package preassembled on a frame and as such they are immediately installed and connected. In contrast to known methods and systems for heat recovery from an exhaust gas stream, it is in particular not necessary to arrange them in a spatially predetermined manner, for example one above the other. The resulting high level of flexibility in system design can save both investment and operating costs.
- the heat is introduced according to the invention by only one heat coupling unit, preferably a heat exchanger, in the thermodynamic cycle. This has the advantage that accordingly only one system component possibly exposed to contamination and corrosion, which further reduces the cleaning effort and thus the operating costs.
- a variant of the method consists in coupling the low-temperature energy into the thermodynamic cycle via a heat exchanger provided directly in the exhaust gas flow.
- the heat exchanger is in this case preferably designed as a straight tube bundle heat exchanger.
- the low-temperature energy is coupled from the exhaust gas flow into the cyclic process via a heat exchanger provided in a circulation or quench water circuit.
- the heat exchanger in the thermodynamic cycle einkoppelnde the heat exchanger is no longer exposed to the possibly polluting and corrosive components such as an exhaust gas flow, whereby contamination or corrosion of the heat exchanger is permanently excluded.
- One possible concrete embodiment is to couple the low-temperature energy into the cyclic process via a heat exchanger provided in the collecting tank of the quench water circuit.
- the heat exchanger may be provided, for example, as a coil heat exchanger.
- thermodynamic cycle of the possibly polluting and corrosive components such as an exhaust stream can be achieved by the low-temperature energy is coupled via a provided in a Quenchigannikank water circuit heat exchanger in the cycle. This can also reduce the quench water temperature at the time of injection.
- thermodynamic cycle can be designed as an evaporator-compressor-condenser-throttle circuit (VVKD circuit), wherein the heat coupling takes place in the evaporator and the heat extraction in the condenser.
- VVKD circuit evaporator-compressor-condenser-throttle circuit
- a VVKD cycle is a closed circuit in which a working medium circulates continuously under state changes (evaporation, compression, condensation, relaxation) and without substance consumption.
- a working medium circulates continuously under state changes (evaporation, compression, condensation, relaxation) and without substance consumption.
- state changes evaporation, compression, condensation, relaxation
- working media commercially available.
- water preferably softened and degassed water.
- novel refrigerants with an increased phase transition temperature are also suitable. The latter is at normal pressure, for example in the range ⁇ 20 ° C, more preferably ⁇ 30 ° C, in particular ⁇ 35 ° C.
- the process may be carried out at a saturation temperature of an exhaust stream of from about 40 ° C to about 80 ° C, preferably 60 ° C to 75 ° C, especially 65 ° C to 73 ° C.
- the evaporation temperature of the working medium in the VVKD circuit at the inlet of the evaporator is preferably about 33 ° C to about 75 ° C, preferably about 46 ° C to 70 ° C, especially 50 ° C to 60 ° C, during the evaporation pressure
- the working medium water at the inlet of the evaporator preferably about 0.05 bar to about 0.40 bar, preferably about 0.10 to 0.30 bar, in particular 0.12 bar to 0.20 bar, or in the refrigerant about 1.0 bar to 3.2 bar, preferably about 1.4 to 3.0 bar, in particular 1.6 bar to 2.2 bar.
- the cycle in the VVKD thermodynamic cycle is set such that the vapor content in the working medium at the inlet of the evaporator is preferably about 5% to
- the pressure of the working medium completely vaporized in the evaporator is in the compressor to a value of about 0.2 bar to about 1.3 bar, preferably about 0.5 bar to about 1.1 bar, in particular about 0.6 bar to 0, 9 bar, or at the refrigerant to 3.5 bar to 5.0 bar, preferably 3.8 to 4.8 bar, in particular 4.0 to 4.5 bar increased, wherein the temperature of the working medium in the compressor preferably by a value of 0 ° C to 250 ° C, preferably 30 ° C to 220 ° C, in particular about 100 ° C to 200 ° C, is increased.
- the compressor preferably operates with an isentropic efficiency of 70% to 90%, preferably about 75% to 85%.
- the compressed working medium passes from the compressor to the condenser, where it is liquefied and gives off heat of condensation to a heat transfer medium, so that the working medium water at the outlet of the condenser preferably a temperature of about 63 ° C to about 108 ° C, preferably about 80 ° C to about 105 ° C, in particular 90 ° C to 100 ° C, or the refrigerant has a temperature of 63 ° C to 108 ° C, preferably 80 ° C to 105 ° C, in particular 85 ° C to 95 ° C. having.
- the heat transfer medium in turn heats up in the condenser by absorbing the heat of condensation of the working medium preferably from a temperature of 50 ° C to 80 ° C, preferably about 65 ° C to 75 ° C, to a temperature of 80 ° C to 100 ° C, preferably about 85 ° C to 95 ° C, on.
- the evaporator can be designed as a spiral heat exchanger or straight tube heat exchanger. Furthermore, the condenser is preferably designed as a steam-water heat exchanger. These are commercially available, proven, because reliable and durable, plant components.
- the VVKD circuit can be provided in the flow direction of the working medium behind the condenser and in front of the throttle an air preheater, which decouples a small part of the heat from the VVKD circuit.
- the preheated in this air is advantageously fed to a not yet completely dehumidified exhaust air flow and contributes there in addition to its Entschwadung.
- the heated air is supplied to the exhaust air flow in the flow direction behind provided in the exhaust duct cleaning stages. In terms of design, this is advantageously achieved in that the supply of the heated air takes place via a central tube. As a result, the contact of the preheated air is maximized with the exhaust air flow to be deswad.
- the thermodynamic cycle is formed as absorption heat pump, wherein the heat input in the evaporator and the heat extraction takes place in the condenser.
- absorption heat pump Such systems are technically mature, known in the market and are used in various branches of technology as heating or cooling machines, are characterized by a high degree of efficiency and longevity and are available in optimized for different applications construction.
- the drive energy for the absorption heat pump here is not electricity, but hot water or steam, which can be removed, for example, in the removal stage of a steam turbine or condensation produced in a gas, biomass or other boiler.
- Thermal oil from production processes can also be used as drive energy - either directly or by transfer to a separate hot water circuit.
- the water is preferably used as the working medium, the water is dissolved in a LiBr solution periodically in an absorber and expelled in an expeller.
- the lithium bromide which acts as an absorbing salt in this case, is a salt which is chemically similar to common salt, but which is very rare in nature occurs.
- the reason for use in absorption heat pumps or chillers is its very high solubility of up to 70% salinity.
- the heat arising during dissolution of the evaporated water in the LiBr solution in the absorber is coupled out as useful heat.
- the heat extraction takes place both in the condenser and in the absorber via a respective heat exchanger, both heat exchangers are part of one and the same Nutznzotigallonss.
- the heat exchangers in the Nutzkorsammlunglauf are serially connected in series. This ensures that the heat transfer medium in the Nutzaginiklauf is gradually increased by each small temperature differences to the desired temperature.
- the low-temperature heat which is taken for example a Quenchwasser mobilislauf
- a heat exchanger which is connected to the Nutzayne Vietnamese Republiclauf.
- Fig. 1 is a device for recovering heat of condensation in a moist exhaust air stream shown, in which the heat is coupled as a low-temperature heat in a thermodynamic cycle, where it is raised to a higher temperature level and is decoupled at the high temperature level as useful heat, at the same time at least part of the the exhaust air contained moisture is condensed.
- the apparatus comprises a horizontally extending exhaust duct which enters a vertically extending exhaust duct 2 passes, to which in turn connects a chimney 3 in the flow direction of the exhaust air.
- a horizontally extending exhaust duct which enters a vertically extending exhaust duct 2 passes, to which in turn connects a chimney 3 in the flow direction of the exhaust air.
- a Gasverteilteil 4
- an electrostatic precipitator 5 for separating solids from the exhaust air flow
- a mist eliminator 6 to avoid drop ejection from the chimney 3, respectively.
- a Quenchingernikonne 7 is provided for cooling the exhaust air flow and thus for condensing out the moisture contained in the exhaust air stream.
- the Quenchinger réellelauf 7 in turn includes one at the foot of the vertically extending
- Exhaust pipe 2 provided Quenchigantoank 8, a Quenchiganpumpe 9 and further in the flow direction of the quench water following, designed as a heat exchanger, preferably as a spiral or Geradrohr Wunschleyer evaporator 10 as part of an even closer to be explained later evaporator-condenser throttle circuit (VVKD -Circuit) 11, optionally also a low-temperature heat exchanger 12 and a number of different locations in the horizontal and the vertical exhaust duct 1, 2 arranged quench nozzles 13.
- VVKD -Circuit evaporator-condenser throttle circuit
- the device still includes a outgoing from the Quenchiganplexank 8 wastewater treatment unit 14, during the operation the device the water Quenchigannikutz 7 can be withdrawn to compensate for the conditional by the continuous Auskondenstechnik of the moisture in the exhaust air flow continuous flow of water to Quenchniklauf 7.
- the already mentioned WKD cycle 11 comprises in addition to the mentioned evaporator 10, which is shown separated from the other components for reasons of clarity, a compressor 15, a preferably formed as a steam-water heat exchanger condenser 16 and a throttle 17. Between the condenser 16 and the throttle 17 is present still an air preheater 18 is provided, in which the heated air via a central tube 19 to the exhaust air stream directly below the chimney 3 can be supplied.
- the quench water sprayed into the exhaust air stream via the quench nozzles 13 then returns, together with the moisture condensed from the exhaust air stream, into the quench water collection tank 8, from which water is released in order to keep the quench water volume constant and the wastewater treatment unit 14 is supplied.
- the softened and degassed water preferably used in the VVKD cycle 11 as the working medium is completely vaporized in the evaporator 10 at a given quench water temperature of 70 ° C. at 0.16 bar (absolute pressure) and 55 ° C. and then in the compressor 15 to higher pressure and higher Temperature compressed, in this case 1 bar and 283 ° C assuming an isentropic efficiency of the compressor 15 of 80%.
- This compression generates superheated steam at 283 ° C and dissipates its heat in the condenser 16.
- a heat transfer medium for example district heating water, heated from 70 ° C to 90 ° C.
- the majority of the heat of the working medium is discharged at a constant 100 ° C until the water vapor is completely transferred into the liquid phase. If the heat of condensation can not be fully utilized for heating the heat transfer medium, it is possible to decouple the then still existing amount of heat in the provided behind the condenser 16 Heilvorier 18 from the VVKD cycle. In the present case, the air heated in the air preheater 18 is supplied via the central tube 19 to the exhaust air stream directly below the chimney 3, thereby additionally contributing to the discharge of the exhaust air flow. It is also possible to use the heat obtained in the air preheater otherwise.
- Fig. 2 illustrated modified embodiment of the apparatus described above differs from this only in that the evaporator 10 'is not in Quenchiganniklauf, ie in the pipe system, but in the Quenchigantrackank 8 is arranged, wherein the evaporator 10' is preferably designed as a coil heat exchanger.
- the advantage of this embodiment is the lower temperature in the wastewater.
- a disadvantage of this embodiment is the slightly worse heat transfer and the risk of contamination and deposits.
- the heat exchanger can also be arranged in the sewer line, in particular between the quench water collection tank 8 and the wastewater treatment unit 14.
- Fig. 3 illustrated embodiment again differs from that of Fig. 1 in that here the evaporator 10 ", which is preferably designed in the form of vertical straight tube bundles, is provided directly in the horizontal exhaust air line 1 and thus directly in the exhaust air flow
- the evaporator 10 is exposed to increased contamination and corrosion. Nevertheless, such an arrangement is particularly suitable for relatively dry, pre-cleaned or little-loaded exhaust gases.
- a device for recovering condensation heat using an absorption heat pump in an exhaust air flow is shown in a schematic view.
- a humid-laden exhaust air stream flowing through from top to bottom is quenched water conveyed in a quench water circuit 21 acted upon, wherein the moisture contained in the exhaust air stream condenses almost completely, so that the exhaust air flow leaves the scrubbing tower 20 with a minimum steam plume.
- the quench water is warmed up to a temperature of approx. 65 °.
- a portion of the quench water is diverted via a separate pump 23 and passed through the evaporator 24 of an absorption heat pump AWP. Subsequently, the quench water is returned to the quench water circuit 21 again. Between pump 23 and the evaporator 24, the approximately 65 ° warm quenching water passes through a further heat exchanger 25, which in turn is connected to a NutzSON Vietnamesesburg, in this case a district heating circuit 26.
- the heat transfer medium of the district heating circuit 26 also passes through the absorber 27 and then the capacitor 28 of the absorption heat pump AWP before it gives off the heat absorbed there to a number of consumers V.
- the drive energy for the absorption heat pump AWP is provided by a gas-fired hot water boiler 29 (power range 3.5-15 MW) with combustion air preheating 29 'and coupled into the expeller 31 of the absorption heat pump AWP via a hot water circuit 30 under overpressure of approximately 10 bar.
- the cooled quench water then passes through the evaporator 24 of the absorption heat pump AWP and evaporates there with a power of about 3.3 MW, the water used in the absorption heat pump AWP as working medium, the quench water continues to cool to a temperature of about 52 ° C.
- the water vapor generated in the evaporator 24 flows via a steam line 24 'to the absorber 27, where it is absorbed by the highly hygroscopic lithium bromide solution.
- the resulting heat of solution is to the heat transfer medium of the district heating circuit 26, which previously in the heat exchanger 25 already by the quench water from a return temperature of max. 55 ° C to about 62 ° C was heated delivered.
- the lithium bromide solution diluted by the absorption of the water vapor is then conveyed by a liquid pump 27 'to the expeller 31, where it is re-evaporated by supplying the heat generated in the hot water boiler 29, i. is concentrated.
- the water vapor formed in the expeller 31 by evaporating the lithium bromide solution is passed through a Steam line 31 '(see. Fig. 5 ) are conducted into the condenser 28. There it is condensed with heat to the heat transfer medium of the district heating circuit 26 and flows as a liquefied working medium via a water pipe 28 'again to the evaporator 24, where it is evaporated again. At the same time, the evaporated lithium bromide solution is pumped back into the absorber 27 via the solution pump 31 ".
- This temperature is now the district heating flow temperature and can be used in contrast to heated to only about 65 ° quench water for a variety of off-site applications.
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- Chemical & Material Sciences (AREA)
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Description
Die Erfindung betrifft ein Verfahren zur Wärmerückgewinnung aus in einem Trocknungsprozess anfallender feuchtebelasteter Abluft, wobei die Wärme als Niedertemperaturwärme in einen als Absorptionswärmepumpe ausgebildeten, thermodynamischen Kreisprozess eingekoppelt wird, dort auf ein höheres Temperaturniveau angehoben wird und auf dem hohen Temperaturniveau als Nutzwärme ausgekoppelt wird und wobei gleichzeitig zumindest ein Teil der in der Abluft enthaltenen Feuchtigkeit kondensiert wird. Zudem betrifft die Erfindung eine Vorrichtung zur Durchführung eines solchen Verfahrens Die Rückgewinnung von Kondensationswärme aus einem Abgasstrom ist bereits aus der Praxis bekannt. Eingesetzt wird es u.a. bei Industrieöfen verschiedener Art, bei Feststofffeuerungen, Trocknern, Rauchgasreinigungsanlagen, Dampf- und Heißwassererzeugern oder ähnlichen Anlagen im industriellen, gewerblichen oder öffentlichen, beispielsweise kommunalen, Bereich. Hier kann die Wärme aus dem Abgasstrom direkt, aus einem den Abgasstrom kühlenden Quenchwasserkreislauf oder aus sonstigem flüssigen Absorbat, wie z.B. Calciumhydroxid in Rauchgasentschwefelungsanlagen, also durch Kondensation bei gleichzeitiger Reinigung der Abgase, gewonnen werden.The invention relates to a method for heat recovery from accumulating in a drying process moisture-laden exhaust air, the heat is coupled as low-temperature heat in a designed as absorption heat pump, thermodynamic cycle, where it is raised to a higher temperature level and coupled on the high temperature level as useful heat and at the same time at least a portion of the moisture contained in the exhaust air is condensed. In addition, the invention relates to an apparatus for carrying out such a method The recovery of heat of condensation from an exhaust gas stream is already known from practice. It is used u.a. in industrial furnaces of various kinds, in solid fuel firing, dryers, flue gas cleaning plants, steam and hot water generators or similar plants in the industrial, commercial or public, such as municipal, area. Here, the heat from the exhaust stream directly, from a Quenchwasserkreislauf cooling the exhaust stream or from other liquid absorbate, such. Calcium hydroxide in flue gas desulfurization, ie by condensation while cleaning the exhaust gases are obtained.
In der
Weiterhin nachteilig an diesem Verfahren ist auch die verhältnismäßig geringe Ausbeute an latenter und fühlbarer Wärme und deren geringes Temperaturniveau, welches weit unterhalb der Sättigungstemperatur des Abgases liegt. Im Normalfall kann die so gewonnene Wärme nicht mehr wirtschaftlich verwertet und daher lediglich über Fernwärmenetze genutzt werden, was zwar ökologisch höchst sinnvollist, bekanntermaßen aber mit zumeist unwirtschaftlich hohem Aufwand für die Bereitstellung entsprechender Leitungsnetze verbunden ist.Another disadvantage of this method is the relatively low yield of latent and sensible heat and their low temperature level, which is far below the saturation temperature of the exhaust gas. Normally, the heat thus obtained can not be used economically and therefore only be used via district heating networks, which is ecologically highly sensible, but is known to be associated with mostly uneconomical high costs for the provision of appropriate networks.
Ein Verfahren der eingangs genannten Art ist beispielsweise aus der
Der Erfindung liegt daher die Aufgabe zugrunde, die Effizienz der Wärmerückgewinnung zu steigern.The invention is therefore based on the object to increase the efficiency of heat recovery.
Die Aufgabe wird erfindungsgemäß mit einem Verfahren gemäss Anspruch 1 und einer Vorrichtung gemäss Anspruch 10 gelöst.The object is achieved by a method according to
Mit dem erfindungsgemäßen Verfahren ist es möglich, die beispielsweise aus einem Abluftstrom gewonnene Wärme auf ein Temperaturniveau anzuheben, womit diese für die verschiedensten innerbetrieblichen Einsatzzwecke genutzt werden kann. Daneben ist natürlich jederzeit auch eine außerbetriebliche Nutzung, beispielsweise als Wärmequelle in einem Nutzwärmenetz, insbesondere einem Fernwärmenetz möglich.With the method according to the invention, it is possible to raise the heat, for example, obtained from an exhaust air flow to a temperature level, whereby it can be used for a variety of internal purposes. In addition, of course, at any time an external use, for example, as a heat source in a Nutzwärmenetz, especially a district heating network possible.
Die für die Ausführung des thermodynamischen Kreisprozesses geeigneten Vorrichtungen können kompakt ausgelegt sein. Im Normalfall werden sie als ein auf einem Rahmen vormontiertes Package geliefert und als solches unmittelbar aufgestellt und angeschlossen. Im Gegensatz zu bekannten Verfahren und Anlagen zur Wärmerückgewinnung aus einem Abgasstrom ist es insbesondere nicht erforderlich, sie in einer räumlich vorgegebenen Weise, beispielsweise übereinander, anzuordnen. Durch die somit gewonnene hohe Flexibilität in der Anlagengestaltung können sowohl investive als auch Betriebskosten eingespart werden.The devices suitable for carrying out the thermodynamic cycle can be made compact. Normally, they are delivered as a package preassembled on a frame and as such they are immediately installed and connected. In contrast to known methods and systems for heat recovery from an exhaust gas stream, it is in particular not necessary to arrange them in a spatially predetermined manner, for example one above the other. The resulting high level of flexibility in system design can save both investment and operating costs.
Die Wärme wird erfindungsgemäß durch lediglich eine Wärmekopplungseinheit, vorzugsweise einen Wärmetauscher, in den thermodynamischen Kreisprozess eingeleitet. Dies hat den Vorteil, dass entsprechend auch nur eine Anlagenkomponente ggf. einer Verschmutzung und Korrosion ausgesetzt ist, was den Reinigungsaufwand und damit die Betriebskosten weiter senkt.The heat is introduced according to the invention by only one heat coupling unit, preferably a heat exchanger, in the thermodynamic cycle. This has the advantage that accordingly only one system component possibly exposed to contamination and corrosion, which further reduces the cleaning effort and thus the operating costs.
Durch die gleichzeitig zumindest zum Teil erfolgende Kondensation der in der Abluft enthaltenen Feuchtigkeit wird eine wirksame Entschwadung (Reduzierung der Dampffahne) der Abluft erreicht.By simultaneously occurring at least in part condensation of the moisture contained in the exhaust air an effective Entschwadung (reduction of the vapor plume) of the exhaust air is achieved.
Hierbei besteht eine Verfahrensvariante darin, die Niedertemperaturenergie über einen unmittelbar im Abgasstrom vorgesehenen Wärmetauscher in den thermodynamischen Kreisprozess einzukoppeln. Der Wärmetauscher ist hierbei vorzugsweise als Geradrohrbündel-Wärmetauscher ausgebildet.Here, a variant of the method consists in coupling the low-temperature energy into the thermodynamic cycle via a heat exchanger provided directly in the exhaust gas flow. The heat exchanger is in this case preferably designed as a straight tube bundle heat exchanger.
Nach einer besonders bevorzugten Ausgestaltung des erfindungsgemäßen Verfahrens ist vorgesehen, dass die Niedertemperaturenergie über einen in einemZirkulations-oder Quenchwasserkreislauf vorgesehenen Wärmetauscher aus dem Abgasstrom in den Kreisprozess eingekoppelt wird. Hier ist somit der die Wärme in den thermodynamischen Kreisprozess einkoppelnde Wärmetauscher nicht mehr den ggf. verschmutzenden und korrosiven Bestandteilen beispielsweise eines Abgasstroms ausgesetzt, wodurch eine Verschmutzung bzw. Korrosion des Wärmetauschers dauerhaft ausgeschlossen ist. Eine mögliche konkrete Ausgestaltung besteht darin, die Niedertemperaturenergie über einen im Sammeltank des Quenchwasserkreislaufs vorgesehenen Wärmetauscher in den Kreisprozess einzukoppeln. Hierbei kann der Wärmetauscher beispielsweise als Rohrschlangen-Wärmetauscher vorgesehen sein.According to a particularly preferred embodiment of the method according to the invention, it is provided that the low-temperature energy is coupled from the exhaust gas flow into the cyclic process via a heat exchanger provided in a circulation or quench water circuit. Here, therefore, the heat exchanger in the thermodynamic cycle einkoppelnde the heat exchanger is no longer exposed to the possibly polluting and corrosive components such as an exhaust gas flow, whereby contamination or corrosion of the heat exchanger is permanently excluded. One possible concrete embodiment is to couple the low-temperature energy into the cyclic process via a heat exchanger provided in the collecting tank of the quench water circuit. Here, the heat exchanger may be provided, for example, as a coil heat exchanger.
Eine noch wirksamere Trennung des Wärmetauschers und damit der den thermodynamischen Kreisprozess ausführenden Anlage von den ggf. verschmutzend und korrosiv wirkenden Bestandteilen beispielsweise eines Abgasstroms lässt sich dadurch erreichen, dass die Niedertemperaturenergie über einen in einem einem Quenchwasserkreislauf nachgeschalteten Wasserkreislauf vorgesehenen Wärmetauscher in den Kreisprozess eingekoppelt wird. Dadurch kann auch die Quenchwassertemperatur zum Zeitpunkt der Einsprühung reduziert werden.An even more effective separation of the heat exchanger and thus the system performing the thermodynamic cycle of the possibly polluting and corrosive components such as an exhaust stream can be achieved by the low-temperature energy is coupled via a provided in a Quenchwasserkreislauf water circuit heat exchanger in the cycle. This can also reduce the quench water temperature at the time of injection.
Die Weiterverwendung der rückgewonnenen und auf ein höheres Temperaturniveau gehobenen Wärme besteht darin, diese als Nutzwärme aus dem thermodynamischen Kreisprozess in einen Nutzwärmekreislauf, insbesondere einen Fernwärmekreislauf auszukoppeln.The further use of the recovered and elevated to a higher temperature level heat is to decouple them as useful heat from the thermodynamic cycle in a Nutzwärmekreislauf, especially a district heating circuit.
Bei einem nicht erfindungsgemäßen Verfahren kann der thermodynamische Kreisprozess als Verdampfer-Verdichter-Kondensator-Drossel-Kreislauf (VVKD-Kreislauf) ausgebildet sein, wobei die Wärmeeinkopplung im Verdampfer und die Wärmeauskopplung im Kondensator erfolgt. Derartige Systeme kommen in den verschiedensten Zweigen der Technik als Wärme- oder Kältemaschinen zum Einsatz, zeichnen sich durch ein hohes Maß an Wirtschaftlichkeit und Langlebigkeit aus und sind in für die unterschiedlichen Anwendungen optimierter Bauweise erhältlich.In a method not according to the invention, the thermodynamic cycle can be designed as an evaporator-compressor-condenser-throttle circuit (VVKD circuit), wherein the heat coupling takes place in the evaporator and the heat extraction in the condenser. Such systems are used in various branches of technology as heating or cooling machines, are characterized by a high degree of economy and longevity and are available in optimized for different applications construction.
Bei einem VVKD-Kreislauf handelt es sich bekanntermaßen um einen geschlossenen Kreislauf, in dem ein Arbeitsmedium stetig unter Zustandsänderungen (Verdampfung, Verdichtung, Kondensation, Entspannung) und ohne Stoffverbrauch zirkuliert. Für derartige Systeme stehen eine große Zahl von Arbeitsmedien kommerziell zur Verfügung. Besonders geeignet, auch vor dem Hintergrund niedrig zu haltender Betriebskosten, ist hierbei der Einsatz von Wasser, vorzugsweise enthärtetem und entgastem Wasser. Alternativ eignen sich auch neuartige Kältemittel mit einer erhöhter Phasenübergangstemperatur. Letztere liegt bei Normaldruck beispielsweise im Bereich ≥ 20°C, besonders bevorzugt ≥ 30°C, insbesondere ≥ 35°C.As is known, a VVKD cycle is a closed circuit in which a working medium circulates continuously under state changes (evaporation, compression, condensation, relaxation) and without substance consumption. For such systems are a large number of working media commercially available. Particularly suitable, even against the background of low maintenance costs, here is the use of water, preferably softened and degassed water. Alternatively, novel refrigerants with an increased phase transition temperature are also suitable. The latter is at normal pressure, for example in the range ≥ 20 ° C, more preferably ≥ 30 ° C, in particular ≥ 35 ° C.
Das Verfahren kann bei einer Sättigungstemperatur eines Abgasstroms von ca. 40°C bis ca. 80°C, vorzugsweise 60°C bis 75°C, insbesondere 65°C bis 73°C, durchgeführt. Dabei beträgt die Verdampfungstemperatur des Arbeitsmediums im VVKD-Kreislauf am Eingang des Verdampfers bevorzugt ca. 33°C bis ca. 75°C, vorzugsweise ca. 46°C bis 70°C, insbesondere 50°C bis 60°C, während der Verdampfungsdruck des Arbeitsmediums Wasser am Eingang des Verdampfers bevorzugt ca. 0,05 bar bis ca. 0,40 bar, vorzugsweise ca. 0,10 bis 0,30 bar, insbesondere 0,12 bar bis 0,20 bar, bzw. bei dem Kältemittel ca. 1,0 bar bis 3,2 bar, vorzugsweise ca. 1,4 bis 3,0 bar, insbesondere 1,6 bar bis 2,2 bar beträgt. Ferner wird der im VVKD-Kreislauf thermodynamische Kreisprozess derart eingestellt, dass der Dampfanteil im Arbeitsmedium am Eingang des Verdampfers bevorzugt ca. 5% bis ca. 15%, vorzugsweise ca. 8%, beträgt.The process may be carried out at a saturation temperature of an exhaust stream of from about 40 ° C to about 80 ° C, preferably 60 ° C to 75 ° C, especially 65 ° C to 73 ° C. The evaporation temperature of the working medium in the VVKD circuit at the inlet of the evaporator is preferably about 33 ° C to about 75 ° C, preferably about 46 ° C to 70 ° C, especially 50 ° C to 60 ° C, during the evaporation pressure The working medium water at the inlet of the evaporator preferably about 0.05 bar to about 0.40 bar, preferably about 0.10 to 0.30 bar, in particular 0.12 bar to 0.20 bar, or in the refrigerant about 1.0 bar to 3.2 bar, preferably about 1.4 to 3.0 bar, in particular 1.6 bar to 2.2 bar. Furthermore, the cycle in the VVKD thermodynamic cycle is set such that the vapor content in the working medium at the inlet of the evaporator is preferably about 5% to about 15%, preferably about 8%.
Der Druck des im Verdampfer vollständig in die Gasphase übergetretenen Arbeitsmediums (Dampfanteil 100%) wird im Verdichter auf einen Wert von ca. 0,2 bar bis ca. 1,3 bar, vorzugsweise ca. 0,5 bar bis ca. 1,1 bar, insbesondere ca. 0,6 bar bis 0, 9 bar, bzw. bei dem Kältemittel auf 3,5 bar bis 5,0 bar, vorzugsweise 3,8 bis 4,8 bar, insbesondere 4,0 bis 4,5 bar erhöht, wobei die Temperatur des Arbeitsmediums im Verdichter bevorzugt um einen Wert von 0°C bis 250°C, vorzugsweise 30°C bis 220°C, insbesondere ca. 100°C bis 200°C, erhöht wird. Hierbei arbeitet der Verdichter vorzugsweise mit einem isentropen Wirkungsgrad von 70% bis 90%, vorzugsweise ca. 75% bis 85%.The pressure of the working medium completely vaporized in the evaporator (steam content 100%) is in the compressor to a value of about 0.2 bar to about 1.3 bar, preferably about 0.5 bar to about 1.1 bar, in particular about 0.6 bar to 0, 9 bar, or at the refrigerant to 3.5 bar to 5.0 bar, preferably 3.8 to 4.8 bar, in particular 4.0 to 4.5 bar increased, wherein the temperature of the working medium in the compressor preferably by a value of 0 ° C to 250 ° C, preferably 30 ° C to 220 ° C, in particular about 100 ° C to 200 ° C, is increased. In this case, the compressor preferably operates with an isentropic efficiency of 70% to 90%, preferably about 75% to 85%.
Das verdichtete Arbeitsmedium gelangt vom Verdichter zum Kondensator, wo es verflüssigt wird und dabei Kondensationswärme an ein Wärmeträgermedium abgibt, so dass das Arbeitsmedium Wasser am Ausgang des Kondensators vorzugsweise eine Temperatur von ca. 63°C bis ca. 108°C, vorzugsweise ca. 80°C bis ca. 105°C, insbesondere 90°C bis 100°C, bzw. das Kältemittel eine Temperatur von 63°C bis 108°C, vorzugsweise 80°C bis 105°C, insbesondere 85°C bis 95°C aufweist. Das Wärmeträgermedium seinerseits heizt sich im Kondensator durch Aufnahme der Kondensationswärme des Arbeitsmediums bevorzugt von einer Temperatur von 50°C bis 80°C, vorzugsweise ca. 65°C bis 75°C, auf eine Temperatur von 80°C bis 100°C, vorzugsweise ca. 85°C bis 95°C, auf.The compressed working medium passes from the compressor to the condenser, where it is liquefied and gives off heat of condensation to a heat transfer medium, so that the working medium water at the outlet of the condenser preferably a temperature of about 63 ° C to about 108 ° C, preferably about 80 ° C to about 105 ° C, in particular 90 ° C to 100 ° C, or the refrigerant has a temperature of 63 ° C to 108 ° C, preferably 80 ° C to 105 ° C, in particular 85 ° C to 95 ° C. having. The heat transfer medium in turn heats up in the condenser by absorbing the heat of condensation of the working medium preferably from a temperature of 50 ° C to 80 ° C, preferably about 65 ° C to 75 ° C, to a temperature of 80 ° C to 100 ° C, preferably about 85 ° C to 95 ° C, on.
Der Verdampfer kann als Spiralwärmetauscher oder Geradrohrwärmetauscher ausgebildet sein. Ferner ist der Kondensator vorzugsweise als Dampf-Wasser-Wärmetauscher ausgebildet. Hierbei handelt es sich um kommerziell verfügbare, bewährte, weil zuverlässig arbeitende und langlebige, Anlagenkomponenten.The evaporator can be designed as a spiral heat exchanger or straight tube heat exchanger. Furthermore, the condenser is preferably designed as a steam-water heat exchanger. These are commercially available, proven, because reliable and durable, plant components.
In dem VVKD-Kreislauf kann in Strömungsrichtung des Arbeitsmediums gesehen hinter dem Kondensator und vor der Drossel ein Luftvorwärmer vorgesehen sein, welcher einen kleinen Teil der Wärme aus dem VVKD-Kreislauf auskoppelt. Die in diesem vorgewärmte Luft wird vorteilhafterweise einem noch nicht ganz entfeuchteten Abluftstrom zugeleitet und trägt dort zusätzlich zu dessen Entschwadung bei. Vorzugsweise wird die erwärmte Luft dem Abluftstrom in Strömungsrichtung hinter in der Abluftleitung vorgesehen Reinigungsstufen zugeführt. Konstruktiv wird dies in vorteilhafter Weise dadurch gelöst, dass die Zuführung der erwärmten Luft über ein Zentralrohr erfolgt. Hierdurch wird der Kontakt der vorgewärmten Luft mit dem zu entschwadenden Abluftstrom maximiert.In the VVKD circuit can be provided in the flow direction of the working medium behind the condenser and in front of the throttle an air preheater, which decouples a small part of the heat from the VVKD circuit. The preheated in this air is advantageously fed to a not yet completely dehumidified exhaust air flow and contributes there in addition to its Entschwadung. Preferably, the heated air is supplied to the exhaust air flow in the flow direction behind provided in the exhaust duct cleaning stages. In terms of design, this is advantageously achieved in that the supply of the heated air takes place via a central tube. As a result, the contact of the preheated air is maximized with the exhaust air flow to be deswad.
Beim erfindungsgemäßen Verfahren ist der thermodynamische Kreisprozess als Absorptionswärmepumpe ausgebildet, wobei die Wärmeeinkopplung im Verdampfer und die Wärmeauskopplung im Kondensator erfolgt. Derartige Systeme sind technisch ausgereift, am Markt bekannt und kommen in den verschiedensten Zweigen der Technik als Wärme- oder Kältemaschinen zum Einsatz, zeichnen sich durch ein hohes Maß an Wirtschaftlichkeit und Langlebigkeit aus und sind in für die unterschiedlichen Anwendungen optimierter Bauweise erhältlich. Als Antriebsenergie für die Absorptionswärmepumpe dient hier nicht Strom, sondern Heißwasser oder Dampf, welches beispielsweise in der Entnahmestufe einer Kondensations-Dampfturbine entnommen oder in einem Gas-, Biomasse- oder sonstigen Kessel erzeugt werden kann. Thermalöl aus Produktionsprozessen kann - entweder direkt oder durch Übertragung auf einen eigenen Heisswasserkreis - ebenfalls als Antriebsenergie verwendet werden.In the method according to the invention, the thermodynamic cycle is formed as absorption heat pump, wherein the heat input in the evaporator and the heat extraction takes place in the condenser. Such systems are technically mature, known in the market and are used in various branches of technology as heating or cooling machines, are characterized by a high degree of efficiency and longevity and are available in optimized for different applications construction. The drive energy for the absorption heat pump here is not electricity, but hot water or steam, which can be removed, for example, in the removal stage of a steam turbine or condensation produced in a gas, biomass or other boiler. Thermal oil from production processes can also be used as drive energy - either directly or by transfer to a separate hot water circuit.
Bei der Absorptionswärmepumpe wird bevorzugt Wasser als Arbeitsmedium verwendet, wobei das Wasser in einer LiBr-Lösung periodisch in einem Absorber gelöst und in einem Austreiber ausgetrieben wird. Das in diesem Falle als absorbierendes Salz fungierende Lithiumbromid ist ein dem Kochsalz chemisch ähnliches Salz, welches allerdings in der Natur nur sehr selten vorkommt. Der Grund für den Einsatz in Absortions-Wärmepumpen oder -Kältemaschinen ist seine sehr hohe Löslichkeit von bis zu 70% Salzgehalt.In the absorption heat pump water is preferably used as the working medium, the water is dissolved in a LiBr solution periodically in an absorber and expelled in an expeller. The lithium bromide, which acts as an absorbing salt in this case, is a salt which is chemically similar to common salt, but which is very rare in nature occurs. The reason for use in absorption heat pumps or chillers is its very high solubility of up to 70% salinity.
Zur Steigerung der Effizienz der Absorptions-Wärmepunpe kann neben der Auskopplung von Wärme im Kondensator auch vorgesehen sein, die beim Auflösen des verdampften Wassers in der LiBr-Lösung im Absorber entstehende Wärme als Nutzwärme auszukoppeln. Bevorzugt erfolgt dabei die Wärmeauskopplung sowohl im Kondensator als auch im Absorber über jeweils einen Wärmetauscher, wobei beide Wärmetauscher Teil ein und desselben Nutzwärmekreislaufs sind. Vorteilhafterweise sind die Wärmetauscher im Nutzwärmekreislauf seriell hintereinander geschaltet. Hierdurch wird erreicht, dass das Wärmeträgermedium im Nutzwärmekreislauf stufenweise um jeweils kleine Temperaturdifferenzen auf die gewünschte Temperatur angehoben wird.To increase the efficiency of the absorption heat pump, in addition to the coupling-out of heat in the condenser, it may also be provided that the heat arising during dissolution of the evaporated water in the LiBr solution in the absorber is coupled out as useful heat. Preferably, the heat extraction takes place both in the condenser and in the absorber via a respective heat exchanger, both heat exchangers are part of one and the same Nutzwärmekreislaufs. Advantageously, the heat exchangers in the Nutzwärmekreislauf are serially connected in series. This ensures that the heat transfer medium in the Nutzwärmekreislauf is gradually increased by each small temperature differences to the desired temperature.
Erfindungsgemäß ist dabei vorgesehen, dass die Niedertemperaturwärme, die beispielsweise einem Quenchwasserkreislauf entnommen wird, in einen Wärmetauscher eingekoppelt wird, welcher mit dem Nutzwärmekreislauf verbunden ist.According to the invention it is provided that the low-temperature heat, which is taken for example a Quenchwasserkreislauf, is coupled into a heat exchanger, which is connected to the Nutzwärmekreislauf.
Die eingangs genannte Aufgabe wird erfindungsgemäß auch durch eine Vorrichtung zur Wärmerückgewinnung aus feuchtebelasteter Abluft gemäß Anspruch 10 gelöst.The object mentioned above is also achieved by a device for heat recovery from moisture laden exhaust air according to
Im Folgenden wird die Erfindung anhand Ausführungsbeispiele darstellender Zeichnungen näher erläutert. Es zeigen:
- Fig. 1
- eine nicht von der Erfindung umfasste Vorrichtung zur Rückgewinnung von Kondensationswärme in einem Abluftstrom unter Einsatz eines VVKD-Kreislaufs in schematischer Ansicht in einer ersten Ausführung,
- Fig. 2
- die Vorrichtung der
Fig. 1 in schematischer Ansicht in einer zweiten Ausführung, - Fig. 3
- die Vorrichtung der
Fig. 1 in schematischer Ansicht in einer dritten Ausführung, - Fig. 4
- eine erfindungsgemäße Vorrichtung zur Rückgewinnung von Kondensationswärme nach dem erfindungsgemäßen Verfahren unter Einsatz einer Absorptions-Wärmepumpe in einem Abluftstrom in schematischer Ansicht und
- Fig. 5
- die Absorptions-Wärmepumpe der Vorrichtung gemäß
Fig. 4 in einer detaillierten Ansicht.
- Fig. 1
- a device not included in the invention for the recovery of heat of condensation in an exhaust air stream using a VVKD circuit in a schematic view in a first embodiment,
- Fig. 2
- the device of
Fig. 1 in a schematic view in a second embodiment, - Fig. 3
- the device of
Fig. 1 in a schematic view in a third embodiment, - Fig. 4
- a device according to the invention for the recovery of heat of condensation according to the inventive method using an absorption heat pump in an exhaust air flow in a schematic view and
- Fig. 5
- the absorption heat pump of the device according to
Fig. 4 in a detailed view.
In
Die Vorrichtung umfasst eine horizontal verlaufende Abluftleitungl, diein eine vertikalverlaufende Abluftleitung 2 übergeht, an die sich in Strömungsrichtung der Abluft wiederum ein Kamin 3 anschließt. In der vertikal verlaufenden Abluftleitung 2 sind von unten nach oben gesehen verschiedene Reinigungsstufen, nämlich ein Gasverteilboden 4, ein Elektrofilter 5 zur Feststoffausscheidung aus dem Abluftstrom sowie ein Tropfenabscheider 6 zur Vermeidung von Tropfenauswurf aus dem Kamin 3, angeordnet.The apparatus comprises a horizontally extending exhaust duct which enters a vertically extending
In der Vorrichtung ist ein Quenchwasserkreislauf 7 zur Kühlung des Abluftstroms und damit zur Auskondensierung der in dem Abluftstrom enthaltenen Feuchtigkeit vorgesehen. Der Quenchwasserkreislauf 7 umfasst seinerseits einen am Fuße der vertikal verlaufendenIn the apparatus, a
Abluftleitung 2 vorgesehenen Quenchwassersammeltank 8, eine Quenchwasserpumpe 9 und weiter in Strömungsrichtung des Quenchwassers folgend, einen als Wärmetauscher, vorzugsweise als Spiral- oder Geradrohrwärmetauscher ausgebildeten Verdampfer 10 als Bestandteil eines im folgenden noch näher zu erläuternden Verdampfer-Verdichter-Kondensator-Drossel-Kreislaufs (VVKD-Kreislauf) 11, optional noch einen Niedertemperatur-Wärmetauscher 12 sowie eine Anzahl an verschiedenen Stellen in der horizontalen und der vertikalen Abluftleitung 1, 2 angeordneter Quenchdüsen 13. Schließlich umfasst die Vorrichtung noch eine vom Quenchwassersammeltank 8 abgehende Abwasserbehandlungseinheit 14, über die während des Betriebes der Vorrichtung dem Quenchwasserkreislauf 7 Wasser entzogen werden kann, um den durch die kontinuierliche Auskondensierung der Feuchte im Abluftstrom bedingten kontinuierlichen Wasserzufluss zum Quenchkreislauf 7 zu kompensieren.
Der bereits erwähnte WKD-Kreislauf 11 umfasst neben dem genannten Verdampfer 10, der aus Gründen der Übersichtlichkeit von den übrigen Komponenten getrennt dargestellt ist, einen Verdichter 15, einen vorzugsweise als Dampf-Wasser-Wärmetauscher ausgebildeten Kondensator 16 sowie eine Drossel 17. Zwischen dem Kondensator 16 und der Drossel 17 ist vorliegend noch ein Luftvorwärmer 18 vorgesehen, bei dem die erwärmte Luft über ein Zentralrohr 19 dem Abluftstrom direkt unterhalb des Kamins 3 zugeführt werden kann.The already mentioned
Die Funktion der Vorrichtung ist die folgende:
- Ein beispielsweise von einer Trocknungsanlage erzeugter feuchtebelasteter Abluftstrom strömt durch die
horizontale Abluftleitung 1, gelangt von dort indie vertikale Abluftleitung 2 und schließlich überden Kamin 3 ins Freie. Der Abluftstrom passiert dabei die in 1, 2 gruppenweise angeordneten Quenchdüsen 13 sowie den in der vertikalen Abluftleitung 2den Abluftleitungen angeordneten Gasverteilboden 4,den Elektrofilter 5 undden Tropfenabscheider 6, wobei die im Abluftstrom enthaltene Feuchte mit einer Rate von beispielsweise 6 m3/h annähernd vollständig auskondensiert, so dass der Abluftstrom ausdem Kamin 3 mit minimaler Dampffahne ausströmt.Die Quenchdüsen 13 werden ausdem Quenchwassersammeltank 8 über diePumpe 9 mit Quenchwasser versorgt, dessenTemperatur im Sammeltank 8 vorzugsweise ca. 70°C beträgt. Vor dem Erreichen der Quenchdüsen 13 durchströmt dasQuenchwasser den Verdampfer 10 sowie den Niedertemperatur-Wärmetauscher 12. In letzterem kann eine zusätzliche Niedertemperatur-Wärmeauskopplung erfolgen, bei dem ein Wärmeträgermedium typischerweise von 40 °C auf 60°C erhitzt wird. Die gesamte Niedertemperaturwärmeleistung beträgt bei einer angenommenen Kondensations-Abwassermenge von 6 m3/ 3,8 MW.h
- An example generated by a drying plant humid exhaust air flow flows through the
horizontal exhaust duct 1, passes from there into thevertical exhaust duct 2 and finally through thechimney 3 into the open. In this case, the exhaust air flow passes through the quenchnozzles 13 arranged in groups in the 1, 2, and theexhaust air lines gas distribution base 4, theelectrostatic precipitator 5 and themist eliminator 6, wherein the moisture contained in the exhaust air stream flows at a rate of, for example, 6 m 3 / h condensed out almost completely, so that the exhaust air flow out of thechimney 3 with minimal steam plume. The quenchnozzles 13 are supplied from theQuenchwassersammeltank 8 via thepump 9 with quench water whose temperature in thecollection tank 8 is preferably about 70 ° C. Before reaching the quenchnozzles 13, the quench water flows through theevaporator 10 and the low-temperature heat exchanger 12. In the latter, an additional low-temperature heat extraction can take place, in which a heat transfer medium is typically heated from 40 ° C to 60 ° C. The total low-temperature heat output is 3.8 MW, assuming a condensation wastewater quantity of 6 m 3 / h.
Das über die Quenchdüsen 13 in den Abluftstrom gesprühte Quenchwasser gelangt sodann zusammen mit der aus dem Abluftstrom auskondensierten Feuchte wieder in den Quenchwassersammeltank 8, aus dem zur Konstanthaltung des Quenchwasservolumens ensprechend der angegebenen Kondensationsrate Wasser abgeleitet und der Abwasserbehandlungseinheit 14 zugeführt wird.The quench water sprayed into the exhaust air stream via the quench
Das im VVKD-Kreislauf 11 als Arbeitsmedium vorzugsweise eingesetzte enthärtete und entgaste Wasser wird im Verdampfer 10 vorliegend bei gegebener Quenchwassertemperatur von 70°C bei 0,16 bar (Absolutdruck) und 55°C vollständig verdampft und anschließend im Verdichter 15 auf höheren Druck und höhere Temperatur verdichtet, vorliegend 1 bar und 283°C bei Annahme eines isentropen Wirkungsgrades des Verdichters 15 von 80%. Durch diese Verdichtung wird überhitzter Dampf mit 283°C erzeugt und dessen Wärme im Kondensator 16 abgegeben. In dem Kondensator 16 wird ein Wärmeträgermedium, beispielsweise Fernwärmewasser, von 70°C auf 90°C erhitzt. Dabei wird der überwiegende Teil der Wärme des Arbeitsmediums bei konstant 100°C abgegeben bis der Wasserdampf vollständig in die flüssige Phase überführt ist. Wenn die Kondensationswärme nicht vollständig zur Erwärmung des Wärmeträgermedium genutzt werden kann, ist es möglich die dann noch vorhandene Wärmemenge in dem hinter dem Kondensator 16 vorgesehenen Luftvorwärmer 18 aus dem VVKD-Kreislauf auszukoppeln. Vorliegend wird die im Luftvorwärmer 18 erwärmte Luft über das Zentralrohr 19 dem Abluftstrom direkt unterhalb des Kamins 3 zugeführt und trägt damit zusätzlich zur Entschwadung des Abluftstroms bei. Auch ist es möglich, die im Luftvorwärmer gewonnene Wärme anderweitig zu verwenden.The softened and degassed water preferably used in the
Nach erfolgter Verflüssigung des Wassers im Kondensator 16 wird dieses in der Drossel 17 entspannt. Diese Entspannung ist mit einer Druck und Temperaturabnahme bis zum Verdampfungszustand (0,16 bar und 55°C) verbunden. Es bildet sich Nassdampf mit einer Dampfziffer von 8%, d.h. einem Dampfanteil von 8%, welcher dem Verdampfer 10 zugeführt und dort wiederum unter Wärmezufuhr verdampft wird, womit der Kreislauf geschlossen ist.After the liquefaction of the water in the
Die in
Die in
In der folgenden Tabelle sind die technischen Daten einer Ausführung des Verfahrens zusammengefasst:
In
In einem Waschturm 20 wird ein diesen von oben nach unten durchströmender feuchtebelasteter Abluftstrom mit in einem Quenchwasserkreislauf 21 gefördertem Quenchwasser beaufschlagt, wobei die in dem Abluftstrom enthaltene Feuchte annährend vollständig auskondensiert, so dass der Abluftstrom den Waschturm 20 mit minimaler Dampffahne verlässt. Bei der kondensation der Feuchte wird das Quenchwasser auf eine Temperatur von ca. 65° aufgewärmt.In a scrubbing
Aus dem Quenchwassertank 22 wird über eine separate Pumpe 23 ein Teil des Quenchwassers abgezweigt und durch den Verdampfer 24 einer Absorptionswärmepumpe AWP geleitet. Anschließend wird das Quenchwasser wieder in den Quenchwasserkreislauf 21 zurückgeführt. Zwischen Pumpe 23 und dem Verdampfer 24 durchläuft das ca. 65° warme Quenschwasser einen weiteren Wärmetauscher 25, welcher seinerseits mit einem Nutzwärmekreislauf, vorliegend einem Fernwärmekreislauf 26 verbunden ist.From the
Das Wärmeträgermedium des Fernwärmekreislaufs 26 durchläuft ferner den Absorber 27 und anschließend den Kondensator 28 der Absorptionswärmepumpe AWP, bevor es die dort aufgenommene Wärme an eine Anzahl von Verbrauchern V abgibt.The heat transfer medium of the
Die Antriebsenergie für die Absorptionswärmepumpe AWP wird vorliegend durch einen gasgefeuerten Heißwasserkessel 29 (Leistungsbereich 3,5 - 15 MW) mit Verbrennungsluftvorwärmung 29' bereitgestellt und über einen unter Überdruck von ca. 10 bar stehenden Heißwasserkreislauf 30 in den Austreiber 31 der Absorptionswärmepumpe AWP eingekoppelt.In the present case, the drive energy for the absorption heat pump AWP is provided by a gas-fired hot water boiler 29 (power range 3.5-15 MW) with combustion air preheating 29 'and coupled into the
Die auf der Lösung von Wasserdampf in einer Lithiumbromid-Salzlösung mit anschließender Austreibung basierende Absorptionswärmepumpe AWP ist in
Die durch die Aufnahme des Wasserdampfs verdünnte Lithiumbromid-Lösung wird sodann von einer Flüssigkeitspumpe 27' zum Austreiber 31 gefördert, wo sie durch Zufuhr der im Heißwasserkessel 29 erzeugten Wärme wieder eingedampft, d.h. aufkonzentriert wird. Der Wärmeübertrag von dem durch den Heißwasserkreislauf 30 geförderten Heißwasser, welches sich im Austreiber 31 von ca. 149° auf ca. 129°C abkühlt, erfolgt mit einer Leistung von ca. 4,1 MW.The lithium bromide solution diluted by the absorption of the water vapor is then conveyed by a liquid pump 27 'to the
Der im Austreiber 31 durch Eindampfen der Lithiumbromid-Lösung entstehende Wasserdampf wird über eine Dampfleitung 31' (vgl.
Das somit zunächst im Absorber 27 und anschließend im Kondensator 28 erwärmte Wärmeträgermedium des Fernwärmekreislaufs 26 wird vorliegend von einer Temperatur von ca. 62°C am Eingang des Absorbers 27 auf eine Temperatur von ca. 90°C am Ausgang des Kondensators 28 erhitzt. Diese Temperatur stellt nun die Fernwärme-Vorlauftemperatur dar und kann im Gegensatz zum auf lediglich ca. 65° erwärmten Quenchwasser für eine Vielzahl außerbetrieblicher Anwendungen genutzt werden.The heat transfer medium of the
Claims (10)
- Method for recovering heat from humid waste air arising in a drying process, wherein the heat is coupled as low-temperature heat into a thermodynamic cycle designed as an absorption heat pump (AHP), is raised to a higher temperature level there and is decoupled at the high temperature level as useful heat, and wherein at the same time at least one part of the moisture contained in the waste air is condensed, characterised in that before coupling the low-temperature heat into the thermodynamic cycle, firstly low-temperature heat is coupled into the useful heat cycle via a heat exchanger (25) connected to a useful heat cycle (26), and in that the heat coupling in of the low-temperature heat takes place in the evaporator (24) of the absorption heat pump (AHP) and the heat decoupling into the useful heat cycle (26) firstly takes place in the absorber (27) of the absorption heat pump (AHP) and subsequently in the condenser (28) of the absorption heat pump (AHP).
- Method according to Claim 1, characterised in that the low-temperature heat is coupled into the thermodynamic cycle via a heat exchanger provided directly in the waste gas flow.
- Method according to Claim 1, characterised in that the low-temperature heat is coupled into the thermodynamic cycle from the waste gas flow via a heat exchanger (24) provided in a quench water cycle (21).
- Method according to Claim 3, characterised in that the low-temperature heat is coupled into the thermodynamic cycle via a heat exchanger provided in the collecting tank of the quench water cycle.
- Method according to Claim 4, characterised in that the heat exchanger is designed as a coil-type heat exchanger.
- Method according to Claim 1, characterised in that the low-temperature heat is coupled into the thermodynamic cycle via a heat exchanger provided in a water cycle downstream of a quench water cycle.
- Method according to any one of Claims 1 to 6, characterised in that water is used as the working fluid in the absorption heat pump (AHP), wherein the water is periodically dissolved in a lithium bromide solution in an absorber (27) and expelled in an expeller (31).
- Method according to any one of Claims 1 to 7, characterised in that the heat decoupling takes place via a heat exchanger provided in the condenser (28) and via a heat exchanger provided in the absorber (27), wherein the heat exchangers are part of a useful heat cycle (26).
- Method according to Claim 8, characterised in that the heat exchangers are serially connected one after the other in the useful heat cycle (26).
- Device for recovering heat from humid waste air according to the method according to any one of Claims 1 to 9, having an absorption heat pump (AHP) performing a thermodynamic cycle, having a useful heat cycle (26) and having a heat exchanger (25) connected to the useful heat cycle (26) for coupling low-temperature heat into the useful heat cycle (26), wherein the absorption heat pump (AHP) comprises an evaporator (24) for coupling low-temperature heat into the thermodynamic cycle, and wherein the absorption heat pump (AHP) has an absorber (27) and a condenser (28) for decoupling heat into the useful heat cycle (26).
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PL07101622T PL1816397T3 (en) | 2006-02-02 | 2007-02-02 | Method and device for heat recovery, from humid exhaust air |
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---|---|---|---|---|
CN112023639A (en) * | 2020-08-26 | 2020-12-04 | 山东国舜建设集团有限公司 | Device and method for recycling latent heat in flue gas treatment of coal-fired power plant |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
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JP5636955B2 (en) | 2010-12-27 | 2014-12-10 | 三菱日立パワーシステムズ株式会社 | Heat recovery system |
FI123697B (en) * | 2012-03-26 | 2013-09-30 | Elomatic Oy | A method and arrangement for transferring heat from a flue gas to a liquid |
CN103512324A (en) * | 2013-09-28 | 2014-01-15 | 昆山市周市溴化锂溶液厂 | Absorption type lithium bromide rapid clean drying system |
NL2011617C2 (en) * | 2013-10-15 | 2015-04-16 | Kea Consult B V | SYSTEM AND METHOD FOR WINNING HEAT FROM A GAS FLOW. |
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CN106248458B (en) * | 2016-09-27 | 2019-03-22 | 阎毅 | Compound gas chamber gas-drying apparatus, drying means and the Apparatus for Dust Content in Stack containing it |
CN106765252A (en) * | 2016-12-23 | 2017-05-31 | 北京建筑大学 | A kind of fountain flue gas waste heat recovery and cleaning system |
CN108106342A (en) * | 2017-12-16 | 2018-06-01 | 安徽热风环保科技有限公司 | Split heat pump hot-blast stove grain drying device |
CN108554086B (en) * | 2018-04-16 | 2021-07-23 | 福建省环境保护设计院有限公司 | High-temperature flue gas purification device |
CN111023134A (en) * | 2019-12-03 | 2020-04-17 | 东南大学 | Heat source tower heat pump for full heat recovery and quality improvement of flue gas waste heat |
FI129538B (en) * | 2020-11-16 | 2022-04-14 | Valmet Technologies Oy | Method and arrangement |
CN113521903A (en) * | 2021-07-08 | 2021-10-22 | 青岛海尔能源动力有限公司 | Distributed energy emission regenerating device |
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DE310352C (en) * | 1915-12-08 | 1900-01-01 | ||
DE2922179C2 (en) * | 1979-05-31 | 1986-05-28 | GEA Luftkühlergesellschaft Happel GmbH & Co KG, 4630 Bochum | Device for temperature control of the drying air passed through a rack when drying agricultural goods |
US4393815A (en) * | 1981-04-16 | 1983-07-19 | Pedersen Niels R | Heating plant |
DE3546465A1 (en) * | 1985-11-02 | 1987-05-14 | Helmut Kohler | Process and arrangement for operating a fuel-burning power station |
DE3631656A1 (en) * | 1986-09-17 | 1988-03-31 | Pauli Balduin | Process and apparatus for improved flue gas purification |
DE3906064A1 (en) * | 1989-02-27 | 1990-08-30 | Boehler Abfall Abluft Abwasser | METHOD AND DEVICE FOR DRYING CRUSHED WOOD |
DE4123556A1 (en) | 1991-07-16 | 1993-01-21 | Fritz Egger Gmbh | METHOD AND DEVICE FOR RECOVERING HEAT FROM DRYING OR EXHAUST AIR PURIFICATION PLANTS |
SE500737C2 (en) * | 1993-03-23 | 1994-08-22 | Lennart Granstrand | Process and apparatus for purifying and extracting energy from hot gas |
AT410180B (en) | 2001-04-12 | 2003-02-25 | Scheuch Gmbh | METHOD AND SYSTEM FOR RECOVERING THE LATENTS AND SENSIBLE HEAT FROM EXHAUST GASES FROM SOLID COMBUSTION |
-
2007
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CN112023639A (en) * | 2020-08-26 | 2020-12-04 | 山东国舜建设集团有限公司 | Device and method for recycling latent heat in flue gas treatment of coal-fired power plant |
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PL1816397T3 (en) | 2015-08-31 |
EP1816397A1 (en) | 2007-08-08 |
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